U.S. patent number 3,853,759 [Application Number 05/091,151] was granted by the patent office on 1974-12-10 for dynamic hydraulic column activation method.
Invention is credited to James A. Titmas.
United States Patent |
3,853,759 |
Titmas |
December 10, 1974 |
DYNAMIC HYDRAULIC COLUMN ACTIVATION METHOD
Abstract
Disclosed is a method and apparatus for promoting chemical
reactions in a hydraulic column, preferably in the form of a well,
provided with an outer casing, an inner liner within and spaced
from the casing, and a steam line within and spaced from the inner
liner. A downwardly flowing column of a material to be treated is
introduced between the casing and the liner and is heated at the
bottom and caused to undergo chemical changes due to the high
pressure and temperature conditions. The reaction zone located
generally at the bottom of the well is maintained free of
extraneous oxygen, that is, free of oxygen except that which might
be inherently entrained in the fluid material. The heated material
is forced upwardly between the liner and the steam line solely by
the column pressure and may be continuously removed at the top,
thus providing a continuous process. If the material being treated
is sewage, it may be provided to the column in its raw state, that
is, not being concentrated or fortified by refuse or other
combustible materials.
Inventors: |
Titmas; James A. (Akron,
OH) |
Family
ID: |
26783646 |
Appl.
No.: |
05/091,151 |
Filed: |
November 19, 1970 |
Related U.S. Patent Documents
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Application
Number |
Filing Date |
Patent Number |
Issue Date |
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735066 |
Jun 6, 1968 |
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Current U.S.
Class: |
210/600; 210/761;
422/198; 422/208; 166/256; 210/762; 422/202; 521/45 |
Current CPC
Class: |
B29B
17/00 (20130101); C02F 1/025 (20130101); C02F
11/083 (20130101); B01J 3/042 (20130101); C02F
1/02 (20130101); Y02W 30/62 (20150501); B29K
2021/00 (20130101) |
Current International
Class: |
C02F
1/02 (20060101); C02F 11/08 (20060101); C02F
11/06 (20060101); B01J 3/04 (20060101); C02b
003/04 (); C02c 001/00 () |
Field of
Search: |
;210/63,64,71,170,177
;166/38-40,300,302,303,57-60,256 |
References Cited
[Referenced By]
U.S. Patent Documents
Primary Examiner: Wyse; Thomas G.
Attorney, Agent or Firm: Hamilton, Renner & Kenner
Parent Case Text
CROSS-REFERENCE TO RELATED APPLICATIONS
This application is a continuation-in-part of my copending
application Ser. No. 735,066 filed on June 6, 1968, now abandoned.
Claims
I claim:
1. A method for treating a continuously flowing sewage material
comprising the steps of, feeding the sewage material into the top
of a hydraulic influent column, conducting said material from the
bottom of said influent column into the bottom of a separate
hydraulic effluent column, continuously supplying heat energy to
the material near the bottom of one of said columns at the reaction
zone to promote chemical reactions and decrease the specific
gravity of the material, limiting combustion of the material by
restricting the process to oxygen present in the material, whereby
the pressure at the bottom of said influent column causes the
heated material to rise in said effluent column, and removing the
material from the top of said effluent column.
2. The method of claim 1, in which the rising effluent column
transfers heat to the descending influent column.
3. A method for treating an oxygen-deficient sewage material
comprising the steps of, continuously feeding the material into the
top of a hydraulic influent column; conducting the material from
the bottom of said influent column into the bottom of a separate
hydraulic effluent column; continuously supplying heat energy to
the material near the bottom of one of said columns at the area of
greatest temperature and pressure to promote chemical reactions to
decrease the specific gravity of the material, and to provide a
pressure differential between the material in said influent column
and the material in said effluent column, the pressure differential
provided by the heat being the sole cause by which the material
rises in said effluent column; limiting combustion of the material
by restricting the process to oxygen present in the material; and
continuously removing the material from the top of said effluent
column.
4. In a process of treating raw sewage material including the steps
of feeding the sewage material into the top of a hydraulic influent
column, transferring said material from the bottom of said influent
column to the bottom of a separate hydraulic effluent column, and
removing the material from the top of said effluent column, the
improvement comprising the additional steps of supplying heat
energy to the material near the bottom of one of the columns so
that the specific gravity of the sewage material will decrease and
the material will rise in the effluent column, and limiting
combustion of the material by restricting the process to oxygen
present in the sewage material.
5. A process according to claim 4, wherein said step of heating the
material is done while restricting the process to combustible
material present in the sewage material.
Description
BACKGROUND OF THE INVENTION
It is well-known that an increase in the speed and efficiency of
many chemical reactions can be induced by subjecting the substances
involved to greatly increased pressure and temperature conditions.
A common example of this would be the household "pressure cooker"
wherein the chemical reactions involved in cooking are accelerated
by use of induced pressure. It has also been found that the
utilization of pressure not only causes substantial yeilds from
processes which could not practically be effected under atmospheric
conditions, but also often eliminates or by-passes undesirable
intermediate by-products which would tend to hamper the primary
reaction objective.
In utilizing the advantageous effects of high pressure on certain
chemical reactions, various ways of attaining the high pressure
have been attempted, such as utilizing a batch-type vessel to
confine the materials which expanded due to the addition of heat,
generally giving off vapors which pressurized the container. This
batch-type reactor was and is deficient in many respects. First,
and most basically, a sufficiently sealed container was not
economically produced. Often the walls of the container tend to
ablate at the seams or otherwise give way to the high pressure.
Further, the batch-type heat expansion system is inefficient in
that little if any of the energy utilized to heat the materials is
recovered.
The obvious response to the problem was the use of a pipe-type
batch reactor or autoclave having a simple closure. However, this
system was complicated with respect to vessel charging and
discharging, there being no practical way of placing the material
to be treated in the pipe, and likewise extracting it upon
completion of the batch process.
Paralleling the development of the heat-expansion batch-type
vessel, was the utilization of a pump to effect the pressures
otherwise effected by the above-described heating arrangement. The
pump system had its advantages in that it could also be utilized to
create a more continuous process, as opposed to the batch concept.
However, the pumping method was limited as it is today, to moving
the fluid materials of a consistent nature; that is, the pump
cannot economically or efficiently handle abrasive materials, or
many other materials in liquid suspension. Also inherent in the
pumping system is the fact that leakage, erosion, corrosion and
cavitation of the pumps themselves make their use quite
limited.
Recently, batch-type reactors have been partially improved through
the development of better sealed, quick opening doors, but remain
limited in pressure and temperature range as well as volume output.
Additional work has been done with continuous-feed reactors, but
these remain inefficient in percentage of yield as well as
frequently requiring costly separation devices. Further, the recent
availability of better pump seals has improved pump applications to
a degree. However, pumps still prove impractical in handling large
volumes of variable density, sometimes abrasive fluids with process
materials in suspension.
One of the applications of high pressure techniques is found in the
treatment of sewage. Since raw sewage can contain most any known
chemical compound, and does contain much objectionable matter which
can best be treated under the aforementioned high pressure
principles, its discussion herein is best used as a representative
example.
Present sewage treatment involves the initial process of separation
by settling of the solid into some type of basin for further
treatment. Many objectionable constituents of sewage defy
separation by this method and in many instances are simply aerated,
or diluted and discharged into natural waters. This handling
technique is normally ineffective in the destruction of appreciable
percentages of the spores of pathogenic bacteria.
The settled solids are concentrated and processed by various
methods, some using high pressure autoclave type techniques.
Presently known methods include digestion, flocculation and
filtration, direct burial, incineration, air drying, wet
combustion, centrifugal separation, lagooning, activated sludge
with recirculation, and others. All of these methods, however, have
the basic disadvantage of being directed only to a relatively small
percentage of the total sewage influent. As alluded to above,
matter in solution, matter in colloidal dispersion, or matter which
by virtue of its specific gravity is unsettleable simple never
reaches the treating mechanism. These categories include living
organisms, fatty acids, protein, cellulose, carbohydrates, and the
volatile hydrocarbons representative of the aforementioned
materials in various stages of decomposition, as well as
precipitated detergent end products, rubber and polyethylene
materials.
Despite the intense use of various systems presently practiced,
these objectional materials persist in accumulation about the human
environment. The abrasive and unpredictable variable nature of
sewage has made large scale high pressure pumping impractical.
Batch autoclaves and vessel reactors are limited in capacity, and
function only for laboratory sterilization and small specialized
treatment situations.
For example, one proposed but not presently commercially acceptable
method of treating waste materials is a wet combustion process
described in U.S. Pat. No. 3,449,247 wherein concentrated sewage is
augmented by the addition of combustion material and provided to a
vertical hydraulic column. Then, utilizing the combustible material
as fuel, oxygen or air is added to the material so that the wet
combustion process may take place. The air further provides an air
lift so that the treated material will rise to the top of a
separate vertical column.
Such a process is, however, limited to high concentrations of
organic material in water. After the wet combustion process has
taken place, the end products are useless and are discarded.
Further, many materials exist in a natural state far too dilute for
practical use in such a process and would require extreme
concentrations or additions of organic material to effect wet
combustion. Working with such concentrations, however, is
intolerable when contemplating a continuous process in a vertical
hydraulic column. The friction losses of these highly viscous
materials result in pressure differentials being such as to cause
collapse of the piping network handling the material.
Further, when the vertical reactor is put into the ground,
installations under this patent would have no means to prevent
escape of process fluids to the surrounding strata or means to
prevent contamination of the process fluids by decomposing the
exposed strata.
Other complications of the method described in U.S. Pat. No.
3,449,247 include multiple deep well drilling; formation of
underground chambers for the storage of air; high residual effluent
pressures; the necessity of preheating the material to begin
combustion; limitations of materials of construction due to
exposure to high temperature combustion; odor control; no means to
recycle the fluid limiting the process to once through
applications; no means to reverse the flow of the fluid; no means
to mechanically mix the materials under peak reactor conditions; no
means to maintain heat transfer effectiveness under low flow
conditions; no means to deter adherence of materials to the piping
apparatus; and no means to introduce energy into the process
without oxidizing materails in suspension or solution.
The treatment of sewage is much like the purification of water to
make it potable; with the latter, the objectionable matter is
vastly diluted. Nevertheless, the system of U.S. Pat. No. 3,449,247
and present techniques with respect to water treatments still leave
the problems of rag and leaf exclusion, grit removal, solids
concentration, organic digestion, solids and waste comutation,
limited design flow range, exposure to the atmosphere, escape of
volitile contaminents, odor control, phosphate and soluble
pollutant removals, excessive land use, aesthetic limitations,
infectious virus transmission, thermal pollution, sensitivity of
bacteriological treatment to industrial spills, dependage on manual
labor for operation, necessity for extensive pipe line transmission
or pumps to raise waste waters above surface waters for gravity
flow through plant, frequent subjection to flooding, necessity for
extensive intercepting collection systems due to inefficient
operation in low flow ranges, infiltration of fresh and sea water
in collection systems, in rush of fresh water from combined
sewerage, and others, which problems remain unsolved.
One other chemical process, utilizing high temperatures and
pressures is the devulcanization of rubber, which is mentioned by
way of example. This has been accomplished to some degree in batch
reactors with some attempts having been made at pumping the
material through pipe reactors. Basically, discarded vulcanized
rubber is ground up, kneaded, and mixed with a catalytic type
substance such as zinc chloride or casutic soda. This material is
then subjected to temperatures and pressures conducive to the
acceleration of breaking the sulfer linking associated with
vulcanization. However, it has been found that the same problems
which plague the high pressure reactor art in general, also plague
the process of devulcanization of rubber in such systems, the
process being slow and limited in batch volume since pumping is
generally prohibitive.
In short, almost any known material which could advantageously be
treated in a high pressure reactor is also subject to the various
shortcomings described above. Further, the teachings of U.S. Pat.
No. 3,449,247 are severely limited to the wet combustion process
which is inherently limited to the treatment of materials wherein
it is advantageous to have oxygen present. Many chemical reactions,
such as the devulcanization of rubber described above, will simply
not satisfactorily occur if oxygen is present.
SUMMARY OF THE INVENTION
It is therefore a primary object of the present invention to
provide a novel method to treat sewage waste material as found in
the environment without the necessity of augmentation or
concentration thereof with combustible refuse and the like.
It is an additional object of the present invention to provide a
method, as above, which will treat sewage waste material and
promote chemical reactions in other oxygendeficient materials
without requiring the addition of oxygen, thereby precluding the
disadvantageous effects of wet combustion.
It is a further object of the present invention to provide a
method, as above, which does not require preheating of the influent
material to be treated.
It is a still further object of the present invention to provide a
method, as above, which utilizes a well-like structure to provide a
vertical hydraulic column without being plagued by direct contact
with the surrounding strata.
It is another object of the present invention to provide a novel
method for treating material utilizing a hydraulic column reactor
which will combine the continuous effect of the pump-type
reactors.
It is another object of the present invention to provide a method,
as above, which can handle large volumes of material while
retaining much of the heat and pressure energy input as well as
increasing yields of known processes.
It is still another object of the present invention to provide a
method, as above, which eliminates the need for a pumping device,
thus facilitating the manner of the charge and discharge
thereof.
It is a further and more specific object of the present invention
to provide a method, as above, adapted for the more efficient, more
economic, and total treatment of sewage and the like.
It is a still further and more specific object of the present
invention to provide a method, as above, adapted to accelerate
chemical processes by use of high pressures and temperatures, such
as the purification of water, devulcanization of rubber, etc.
These and other objects which will become apparent from the
following specification are accomplished by means hereinafter
described and claimed.
In general, the apparatus employed to promote the desired chemical
reactions consists of a hydraulic column to provide the
reaction-inducing high pressure, and a means to provide heat energy
to the bottom of the hydraulic column. The preferred manner of
obtaining the high pressure is by utilizing a deep well having
casing to conduct the material downwardly and a liner spaced within
the casing to return the material to the surface. A steam line or
other heating means is spaced within the liner to supply the
necessary heat energy at the bottom of the column.
Means are provided within the casing for the injection of a
catalyst at any depth, should the process require it. At the bottom
of the well, the material is directed from between the outer casing
and the liner into the bottom of the liner. This area is heated by
steam or another media and the desired chemical reactions are thus
promoted or accelerated. Since no extraneous air, oxygen or
combustible refuse is provided to the column, the disadvantageous
effects of wet combustion can be avoided. The heated substance,
being lighter than the denser and cooler influent, is caused to
flow up within the liner. As the warm effluent passes by the cool
influent, some of the heat is transferred through the liner from
the effluent to warm the influent. Thus, not only is a continuous
process assured, but also much of the heat energy supplied is
conserved and passed on to the influent.
BRIEF DESCRIPTION OF THE DRAWINGS
FIG. 1 is a somewhat schematic elevational view of a preferred
embodiment of the apparatus of the invention, parts being broken
away and in section.
FIG. 2 is a top plan view thereof.
FIG. 3 is a schematic flow diagram of a preferred embodiment of the
invention.
FIG. 4 is a graphic illustration of representative pressures and
temperatures of a material as it is being treated.
FIG. 5 is an enlarged sectional view of the apparatus at the bottom
of the hydraulic column according to a preferred embodiment of the
present invention.
FIG. 6 is an enlarged view of the liner within the outer casing
showing the liner stabilizer according to a preferred embodiment of
the present invention.
FIG. 7 is a sectional view taken substantially along line 7--7 of
FIG. 6.
FIG. 8 is a schematic representation of the expansion device
employed according to a preferred embodiment of the present
invention.
DESCRIPTION OF THE PREFERRED EMBODIMENT
The apparatus according to the present invention is designated
generally as numeral 10 in FIG. 1. A preferred manner of creating
the hydraulic head necessary to accomplish the objectives of the
present invention is the utilization of a well indicated generally
as 11, of a prescribed depth which, of course, would vary according
to the pressure needed for the particular chemical reactions
contemplated. Well 11 consists of a bore 12 into which is fitted a
well casing 13. Concentric of casing 13 is a liner 14 of smaller
diameter than casing 13. Concentric of and spaced within liner 14
is a heat energy or steam line 15 which, as shown in FIG. 5, is
preferably encased by an insulating sleeve 16 through the majority
of its length so that the heat energy in the form of steam will not
be lost to the surrounding environment. Steam line 15 is therefore
utilized to provide the heat energy necessary for the chemical
reactions desired. However, it should be evident that other forms
of heat energy, such as electricity, might well replace the steam
energy in certain installations.
The bottom of the well 11 is best shown in FIG. 5 as being closed
off to the strata by a cement or grout 18, which can hold the
casing 13 in place. Slidably received within casing 13 is a
circular base member 19 having an outer annular flange 20 and
resting on the grout 18. Base member 19 further provides an
additional barrier to prevent significant contact of the fluid
medium with the strata or with the grout system 18. Flange 20 of
base 19 is provided basically for strength, base 19 being designed
of a material having high corrosive and erosive resistance. Base 19
further has a center upright leg 21 which provdes a seat for the
bottom of steam line 15, steam line 15 being preferably welded
thereto. Welded to base leg 21 is a spider 22 which has a plurality
of radial branches providing outer shoulders 23 on which rest an
outwardly tapered annular extension 24 of the bottom of liner 14.
Extension 24 not only provides a mating face to rest on shoulders
23, but also serves to form a venturi zone to ease pressure losses
at the reverse flow point as will hereinafter become evident.
Interiorly fastened to the liner 14 at the upper end of extension
24 is an annular ring 25 which is mounted, as shown in FIG. 5, in a
plane transverse to that of the liner 14. Similarly, a smaller ring
26 is attached exteriorly of steam line 15, creating a restricted
orifice 28. Rings 25 and 26 are shaped in cross-section like a
parallelogram having no right angles therein. This is done so that
even though the rings do not rest in a plane perpendicular to the
liner 14, their surfaces 27 are nevertheless parallel to the liner.
Orifice 28 is adjustable in size by mere rotation of liner 14. As
shown, orifice 28 would be at its smallest extent; however,
rotation of liner 14 by 180.degree. to the chain line position
would open orifice 28 to its greatest extent. Orifice 28 can thus
be adjusted to provide the desired amount of mixing action in the
effluent passing through spider 22 upwardly into liner 14.
Steam line 15 is provided with a plurality of discharge jets 29
which direct steam toward orifice 28. It is at approximately this
area where the most rapid chemical reaction will take place, it
being the area of greatest pressure and temperature in the
system.
The assembly of these various components into well 11 should now be
evident. Casing 13 is first set in grout 18 and the steam line is
lowered with the base 19 attached thereto. Liner 14 is then lowered
and extension 24 placed on shoulders 23 of spider 22. Finally an
additionally grouting material 30 is packed around casing 13 within
well bore 12. Grout 30 can be dry sand or powdered cement or a
cement slurry mixture with additives for thermal stability and
insulation purposes and is utilized to equalize the pressure inside
and outside the casing. Grout 30 thus protects the casing from the
eventual pressures of the strata and also acts as an insulation
material.
Above ground level, liner 14 is shown extending through the top
elbow of casing 13; therefore, a seal at 31 must be provided.
Similarly, another seal at 32 is required where steam line 15
extends through the top elbow of liner 14. The seals 31 and 32 may
be of a conventional construction. Steam line 15 then continues to
a conventional steam generator (not shown).
In the discussion of the preferred embodiment, the process of
devulcanizing rubber may be used as representative of many other
treatments which system 10 is capable of accomplishing. In this
instance then, the discarded rubber to be treated is ground up into
small bits and placed in a carrying medium which may be water or
which in the devulcanization of rubber example may be a zinc
chloride brine or caustic soda. In this manner, the conveying
medium would aid the reaction with its catylitic effect. As will
hereinafter become more evident, when a conveying medium other than
water is utilized, it is possible and often desirable to provide in
line 15 the vapor of the conveying medium as the heat energy. Of
course, when water is the conveying medium, steam would be the most
efficient form of heat energy.
The mixture of ground rubber and water or catylitic brine is
supplied to an influent tank or line 33 as shown in FIGS. 1 and 2.
Referring generally to FIGS. 2 and 3, provisions have been made so
that the influent rubber in suspension coming from line 33 may
by-pass the entire system. This is shown in FIG. 2 as an open
by-pass channel 34 having control gates 35 and 36 at the inlet and
outlet thereof respectively. While being shown as open channels, it
is evident that any medium, such as a pipe, would be sufficient.
Thus in the schematic FIG. 3, a simple by-pass line is shown having
a normally closed valve 38. This by-pass system could be utilized,
for example, either in times of emergency, as in system overflow or
breakdown, or in other situations where by-pass might be
desirable.
If by-passing is not desired, the influent will then pass through
gate 39 of FIG. 2 (normally open valve 40 of FIG. 3), and through a
screening device 41. Screen 41 assures that no oversize particles
of rubber reach the hydraulic column itself. Another normally open
valve 42 may be provided after screen 41. At this point it has been
found desirable to provide a classifier 43 (FIG. 3) which acts to
segregate materials by specific gravity to eliminate overly dense
or large undesirable particles which may have been passed the
sizing test afforded by screen 41.
In the embodiment of FIG. 1, an above-the-ground lateral extension
44 of casing 13 is provided through partition walls 45. Casing
extension 44 is connected to a downturned pipe 46 which serves in a
siphon-like manner to pick up the influent rubber in suspension. A
classifier, similar to that discussed with reference to FIG. 3, is
thus provided at the mouth 47 of pipe 46. Mouth 47 acts like a
siphon and will pick up only those particles which are light
enough, thus eliminating overly dense materials. Further provided
therein is a bar 48 which acts not only to help stabilize the
system, as will hereinafter be discussed, but it also duplicates
the conditions found in the well 11 compensating by velocity
selection design for the change in viscosity of the carrying fluid
at the reverse flow point in the hydraulic column and thus assures
that oversize and overweight particles will not clog the system.
Bar 48 also provides a means for regulating the uptake force of
mouth 47. A large bar will increase the uptake suction velocity at
mouth 47, due to the decrease in the relative area of mouth 47.
The influent rubber in suspension should now be ready to enter into
the hydraulic column, or what has been previously referred to
generally as well 11. The influent flows by gravity down in the
area defined by the inside of casing 13 and the outside of liner
14. Preferably, there is provided in this passage a plurality of
influent probes 49 shown in FIG. 1, which are, in effect, long
adjustable pipes or tubular members of small diameter which can be
used to take off a sample of the influent at any desired depth, or,
more importantly, can be used to add catalytic chemicals at the
exact pressure and temperature condition needed. Thus in the
present instance, it would be desirable to add zinc chloride or
caustic soda to the influent rubber in suspension. These substances
will, at the right temperature and pressure, tend to break the
sulfur bond associated with vulcanization. It should be noted that
while these substances may be added in tank 33, classifier 43, or
at any point of influent travel, the probes provide for
introduction of the chemical substances under the most effective
temperature and pressure conditions.
As previously alluded to, well 11 may be designed both in depth and
in cross-sectional area according to the use for which it is
intended. For whatever use, however, the peak temperature and
pressure conditions will be found at the bottom in the area of
orifice 28 and jets 29. Referring to FIG. 5, the influent under
hydraulic column pressure is directed by shoulder 24 and base 19 up
through spider 22 toward orifice 28 whereupon it is instantly
contacted by the extreme heat of the steam from jets 29. This heat
and pressure combined with the injected chemical agents causes a
substantial devulcanization of the rubber in suspension.
Since the devulcanization of rubber must be accomplished in the
absence or near absence of air, care must be taken to assure that
very little air is entrained in the influent supply. Otherwise, the
heat and pressure conditions achieved by this system would cause
combustion, burning the rubber and leaving no usable end product.
Thus, the influent must be oxygen-deficient, that is, not have
enough oxygen to cause substantial combustion. By keeping the
reactoin zone free of extraneous oxygen, that is, oxygen added in
the process, this result can be achieved.
The treated material, now being heated and lighter, will be forced
up the area between liner 14 and steam line 15 as the sole result
of the change in density of the material. The air-lift
characteristic of the prior art is not necessary (nor desirable, as
described above). Thus, a continuous movement of the system is
provided.
It should be evident that the substantially warmer effluent treated
rubber in suspension will tend to heat the influent non-treated
rubber in suspension via conduction through the walls of liner 14.
For these purposes, liner 14 should be relatively thin or made of a
material which will readily transfer heat. Further, if the liner is
sufficiently thin, it may be flexed by flow reversal to crack off
adhering brittle materials.
Thus after the initial "start-up" conditions, the essentially cold
influent will be warmed throughout its downward journey by the
relatively hot effluent which is moving upward. As will hereinafter
be more specifically explained, and as now should be apparent, most
of the heat energy provided by the steam is thus conserved within
the system. Further, the high pressure is constantly maintained at
no extra cost due to the hydraulic column.
By the time the effluent reaches the top of well 11 it will be
substantially cooled having passed much of its heat to the oncoming
influent. However, a recirculation channel 50 is preferably
provided at this point, should it be desired to capture whatever
heat remains in the effluent treated rubber solution or should it
be desirable to provide a means which would permit a reversal in
flow of the entire system. As shown in FIG. 2, the recirculation
system may be an open channel with a control gate 51 and separating
device 52, or as schematically shown in FIG. 3, it may be a piping
system having a normally open valve 53 which allows the material to
enter a separator 54. Both separators 52 or 54 are designed to take
off the devulcanized rubber and allow the warm carrying medium and
any remaining vulcanized rubber to continue back through the system
again. This is accomplished since devulcanized rubber tends to be
lighter than vulcanized rubber, the former thus tending to move
toward the top of the separator to be taken off there, and the
latter gravitating to the bottom to be fed with the warm water
through a variable valve 55 and back to classifier 42 for further
treatment.
Should recirculation not be desired, either valve 53 or 55 could be
closed and, in the channel form of FIG. 2, outlet control gate 56
be opened, or in the schematic form of FIG. 3, either or both of
valves 58 opened. This would open the effluent to a screen or
series of filters 59 which would act like separator 54 in selecting
the desired product and emitting it through either or both of
valves 60. Note that two filters are provided so that one can be
used while the other is being cleaned of the materials via backwash
valves 61. Also provided at the downturned end of liner 14 is an
adjustable sleeve member 58 (FIG. 1) which regulates the back
pressure in liner 14. As sleeve 57 makes liner 14 larger (and thus
closer to the bottom of the tank shown), more back pressure in
liner 14 is provided, should it be desirable.
Referring generally to FIG. 8, it has been determined that due to
the high heat involved in the system, compensation should be made
for pipe expansion. Shown in FIG. 8 is one example being applied to
the steam line. There, the top of steam line 15 has conventional
pipe elbow joint 62 which holds articulating arm 63. The other end
of arm 63 is connected by another joint 64, arm 63 and steam line
15 thus being connected to the steam generator 65. As steam line 15
heats up and expands, arm 63 moves from the chain line position to
the full line position of FIG. 8 by rotation at joints 62 and 64.
By varying the length of arm 63, most any pipe expansion can be
accounted for. Since arm 63 must be quite long in certain
instances, springs 66 are provided to alleviate any binding
stresses at joints 62 and 64 due to the weight of arm 63. One
alternative method of compensating from the pipe expansion would be
to provide conventional expansion means between each length of pipe
in the steam line itself. By utilizing this concept, each joint
would have to account for a small fraction of total pipe expansion.
Another alternative would be to provide a "hanging" liner 14, that
is, suspend the cold liner above the shoulder 23 of spider 22 and
allow it to "grow" downward when heated. The hanging liner, as well
as seated liner for that matter, would be readily adaptable to
facile raising and lowering which would aid in maintaining the
liner free of undesirable materials.
Also, as seen in FIG. 6 and 7, each pipe union of liner 14 has a
system of stabilizers 68. The stabilizers consist of spirally
curved lengths of rod which are welded, as at 69, at each pipe
junction, and which rest against either the casing at 70 or steam
line at 71. In effect these rods are spring loaded in that their
force against the casing and steam line tend to keep the whole
piping system centered on installation and during use. Further,
these stabilizers will not only tend to dampen vibrations which
might occur, but also provide a plurality of obstructions in the
path of both the influent and effluent, which obstructions tend to
mix the flow and keep the pipes clean. Stabilizers are also
provided at the mouth 47 of pipe 46 for similar purposes.
Being obstructions to the flow, that is, being placed angularly to
the flow of the material, it is evident that the stabilizers 68 can
be designed to perform the additional function of turning or
rotating the liner by a paddle wheel effect. This rotation would
not only deter adherence of materials to the liner and break liner
surface film and thereby improve heat transfer characteristics, but
when in the path of the effluent, stabilizers also favorably
utilize the excess head that may be present therein, as will
hereinafter be described.
Having now discussed the system 10 in general terms with respect to
the process of devulcanizing rubber, it would be best to define
various parameters of such a devulcanization system. While
devulcanization will occur at 350.degree. F. under a pressure of
600 psi, it has been determined that a more rapid devulcanization
will occur at a temperature of 500.degree. F. under a pressure of
1,000 psi. It would thus be desirable to obtain these conditions at
the bottom of the hydraulic column.
In order to achieve a pressure of 1,000 psi, a well of
approximately 2,300 feet would be required. A system of this depth
is calculated to handle 5,000 pounds of rubber dispersed in 50,000
pounds of water each hour with an outer casing of at least 9 inch
diameter, a liner of about 6 inch diameter, and steam line of about
3 inch diameter.
While the securing of the required pressure is thus only a function
of depth, the heating requirements are somewhat more complex. For
example, heat gains are derived from the steam itself, from pipe
friction, and from exothermic reactions. Heat losses involved are
those to the strata, those due to condensation in the steam feed
line and those which account for the terminal temperature
difference. Finally, heat transfers from effluent to influent must
be considered.
The losses attributed to the strata are considered first. Of
course, the well site should be a comparatively dry one, for if
not, the heat would be quite readily carried off by any present
moisture. Assuming relatively dry strata, the heat losses to the
strata may be described as the instantaneous heating of an
infinitely thick wall. The heat losses are found to be inversely
proportional to the square root of time (in hours) so that while
never reaching zero, it is evident that the losses become minimal
after a short period of time. In fact, it is only during "start-up"
and shortly thereafter that the losses are appreciable. After that,
the heated strata actually acts like an insulator. If it were
desired to minimize initial losses to the strata, an adequate
insulating material could be packed around the outer casing in
place of the grout material. However, one would have to weigh the
cost of this insulation versus the cost of providing extra steam at
the initial stages of the process. Due to the relative economic
ease of steam production, it would seem that the latter choice
would be preferred.
In the example under discussion, it has been calculated that the
losses after 1 year would be approximately 50,000 BTU per hour;
after 2 years 33,000 BTU per hour; and after 3 years 26,000 BTU per
hour. In steam output, this would mean a consumption, at the 1 year
point, of about 77 pounds per hour.
Continuing the example, assuming heat losses after 1 year (since it
is recognized the initial heat losses would be greater and those
later would be lesser), it is found that if the influent
temperature is 195.degree. F. (obtained from recirculating warm
effluent), and if the peak temperature condition is 500.degree. F.,
the effluent will reach the top of the well at about 211.degree.
F., thus cooling from 500.degree. F. to 211.degree. F. The
289.degree. F. difference is, of course, largely transferred from
the effluent to the influent through the liner, which in terms of
BTU's amounts to 905,000 BTU/.degree.F-Hour. Thus there is a
terminal temperature difference of about 16.degree. F., which
difference, when expressed in terms of steam consumption, means
about 1,270 pounds of steam per hour.
The loss due to condensation in the steam line has been calculated
at about 91,500 BTU per hour which means about 141 pounds of steam
per hour. Note that in this regard, it has been mentioned that the
steam line should be insulated. The reason for this is to prevent
over-condensation as the steam travels down the line, and to
prevent a heat loss from the steam line to the effluent. The net
result is that the maximum steam can be provided at the maximum
depth with only 141 pounds of steam lost each hour to
condensation.
The total losses then (strata: 77; steam condensation: 141; and
terminal temperature difference: 1,270) amount to 1,488 pounds of
steam per hour needed after 1 year's use. A steam generator with an
output of 3,000 pounds per hour would thus be adequate, in this
example, for "start-up" and all subsequent conditions.
It has been found that when considering heating requirements of the
above described magnitudes, both of the heat gains alluded to above
become negligible. For example, the heat gain from friction would
amount to about 700 BTU/hour, or about a savings of 1 pound of
steam per hour. Thus, while prior art devices utilize the heat from
the reaction to maintain the combustion of the fortified sewage
material, these heat gains are so insignificant to the present
device that they are deemed negligible.
The friction loss does play an important role, however, as a
deterent to the thermal head which provides the motive force in the
system. The differential thermal head, that is, the motive force in
this example, has been calculated at approximately 10 psi. However,
the total friction losses amount to about 10.5 psi. Therefore, in
this particular example, either a static head would have to be
created, i.e., raise the level of the influent, or a very small
amount of steam be added over the saturation requirements. In the
latter situation, the addition of a very small amount of steam
significantly increases the head. This is due to the fact that any
steam injected over saturation will remain as steam in the
effluent, and thus substantially lighten the effluent and cause a
greater flow therein. Therefore it is evident that the amount of
steam controls the flow rate in the system. In the example above,
the total flow time, as regulated by the steam, was only 59
minutes.
The overall temperature-pressure conditions in the system just
described can be best seen in the graphic representations of FIG.
4. The screen device 41 causes a slight pressure drop due to the
slight resistance which it presents to the influent. A
representation pressure drop of 1 psi is shown. Similarly, a small
pressure drop occurs in the classifier. Then as the material passes
into the casing of the well, the maximum point is reached. Of
course, at this point the pressure will fluctuate somewhat
radically due to the fluid flow around the reversal point and
through the orifice. Then, as the material moves up the liner, the
pressure decreases until the material is expelled at a pressure,
which, of course, varies as a function of the thermal head
involved. In the example given above, it is assumed that enough
extra steam has been added to give the 30 psi output pressure shown
in FIG. 4. Then the pressure drops again at the filter area before
being ejected.
The temperature at these various points is shown on the lower graph
of FIG. 4. The influent temperature remains fairly constant after 1
year, except for the small increase due to the recirculation input,
until reaching the hydraulic column. There as it passes by the warm
liner, it gains heat progressively until it reaches the bottom when
the temperature is "bumped" up by the steam injection. Then the
effluent loses its heat to the influent until it reaches the top of
the column. There it is taken off at a slightly higher temperature
(in this example 16.degree. F.) than the influent. This warmer
effluent can either be merely ejected from the system and the heat
lost to the atmosphere, or it can be recirculated to mix with the
cooler influent.
TREATMENT OF SEWAGE
The use of the above-described apparatus in treating sewage is
important since raw untreated sewage, obtained naturally from
cities and the like and unfortified by combustible refuse or oxygen
can contain many materials, most of which are undesirable and most
of which can be purified by the use of a high pressure and
temperature environment. Further, raw sewage lends itself to this
apparatus since it already consists of a great deal of water which
will act as its carrying medium, and since it must be handled
efficiently in large volumes.
While there may be entrained oxygen and/or combustible material
present in naturally occurring sewage, an advantage of the present
process, particularly when treating sewage, is that extraneous
oxygen and refuse is not present in the reaction zone. That is, the
present process does not require the affirmative step of adding
oxygen or refuse extraneous to that small amount which may be
inherently present in the material as it is provided to the
hydraulic column 10. Of course, as previously described, processes
which do require such procedures are at a decided disadvantage.
However, denying oxygen to the reaction zone having a minimum of
combustible refuse present does not allow the reaction to be taken
over by the wet combustion process. Naturally occurring unaugmented
sewage is simply too oxygen-deficient for such to occur.
The treatment of sewage, nevertheless, is very much like the
devulcanization of rubber, however, many of the steps become more
critical and others may be eliminated. Initially, raw sewage from a
community would be directed to the influent tank 33. The screening
device 41 and bar 48 become important in this instance since the
size of the particles in sewage cannot be controlled as readily as,
for example, in the devulcanization of rubber.
The by-pass provisions are also helpful in the sewage situation,
for example, to shut down the system for cleaning. Just as before,
if not by-passed, the sewage would pass through the classifier 43
and onto the hydraulic column. Probes 49, which as discussed above,
can be positioned at any height within the influent or effluent,
are quite effective as samplers in the process of treating sewage.
However, in general, since no chemical is ordinarily added in this
process, the step of adding a catalyst may be eliminated in this
instance. But, it may be necessary, for example in a community
having vast industrial wastes in its sewage, for certain chemicals
to be added to aid in the purification. Probes 49 are thus useful
in this situation. A probe entering the cooler zones of the
effluent may be utilized to introduce a refrigerant compressed gas
to be cooled and condensed by direct contact with the fluid. Upon
throttled discharge at control 57, the refrigerant would boil and
extract heat from or after-cool the effluent. The gas could then be
recovered by separation for recompression and recycle.
When peak temperature and pressure conditions occur (at the bottom
of the well), the breakdown of the various undesirable materials,
particularly those materials in suspension and colloidal
dispersion, occurs. This system is advantageous in that except for
the rough initial screening, the entire influent is treated
chemically and physically by subjection to peak process conditions
which are most efficiently over 1,800 psi and 635.degree. F. The
time, temperature and pressure duration is intended to provide
substantial hydrolysis of various fatty acids; sterilize pathogenic
material; decompose meat proteins; pyrolize materials such as
hydrocarbons; hydrogenize or carbonize cellulose, and others.
Since the natural environment of sewage is the liquid carrying
medium, it would not be at all mandatory that the recirculation
channel 50 be used. However, such a channel would be useful during
a starting "warm-up" period and during periods of low sewage flow
rates. Normally, however, the sewage effluent would usually pass to
filters 59 and then into some natural water source such as a river
or lake. Should some of the objectionable matter remain, however,
the recirculation system could be utilized to return the effluent
to recirculate through the system.
The parameters of the sewage treating system are similar to those
in the devulcanizing system except that since a desirable peak
pressure in 1,800 psi and temperature is 635.degree. F., a
substantially deeper well of about 4,600 feet is needed. Further, a
much larger diameter well is needed to handle greater volumes. For
example, the standard treatment plant of the Public Health Service,
serving a town of a 5,000 population, requires that 500,000 gallons
of sewage be treated each day. To treat this volume, a casing of
approximately 14 inches, liner of 10 inches, and steam line of 4
inches would be necessary.
Just as in the devulcanization of rubber, the heat losses, gains,
and transfers must be considered. Assuming relatively dry strata,
the heat lost to the strata after 1 year in this example would be
approximately 115,000 BTU per hour, which would mean a steam
consumption of 250 pounds per hour lost to the strata.
Without recirculation, the average influent temperature of sewage
is about 50.degree. F. Note that this is substantially less than
the 195.degree. F. in the influent rubber situation. After the
50.degree. F. sewage reaches the 635.degree. F. peak condition, it
will cool until it exists at about 84.degree. F. The 551.degree. F.
temperature difference is, of course, transferred directly to the
influent. Thus there is a terminal temperature difference of about
34.degree. F., which difference translated into steam consumption
means about 13,150 pounds of steam per hour. This steam consumption
could obviously be reduced by increasing the heat transfer area of
the liner if desired as by providing fins as would be well known to
one having ordinary skill in the art.
The additional heat or power loss due to condensation in the steam
line has been calculated at about 349,000 BTU per hour or about 754
pounds of steam per hour.
The total losses, or the energy consumed, for this example then
amount to 14,152 pounds of steam per hour. Again the heat gained
from friction and the various exothermic reactions involved can be
considered negligible considering the sizable amount of heat needed
in this process.
The friction loss, however, would have an important effect on the
thermal head created by the terminal temperature difference which
provides the motive force of the system. Disregarding the friction
loss, the thermal head would be about 87.2 feet considering the
relative influent and effluent densities. However, the friction of
the effluent going up the well reduces that head by an equivalent
of 41.4 feet thus leaving a remaining head of 45.8 feet. As
previously described, through the advantageous use of the
stabilizers 68, much of the force of this thermal head can be used
to rotate the liner and promote cleaning, and heat transfer, and is
generally a source of mechanical energy. Nevertheless, due to the
more drastic terminal temperature difference in this example, a
much larger motive force is created and even though the well is
twice as deep, the flow time is only 80 minutes.
It should now be evident that the apparatus and method herein can
be adapted for any desired use by a mere change in system
parameters and possibly slight changes in chemical additives. This
system can be utilized to effect an unlimited number of chemical
processes which are aided by high pressure. As examples, the
chemical reaction known as pyrolysis (the destructive distillation
of organic material in the absence of air) is one of the major
chemical reactions which takes place in the purification of sewage
and can be maintained at minimum temperature and pressure
conditions of 550.degree. F. and 1,000 psi; alkylation (the
replacement of a hydrogen atom with an alkyl group in an organic
compound) will take place at a temperature of at least 266.degree.
F. and a pressure of at leat 200 psi; hydrolysis (combination of
greases and the like with water to normally form an alcohol and
acid) will take place at a temperature of at least 480.degree. F.
and a pressure of 600 psi; and hydrogenation (the addition of
hydrogen to the molecule of an unsaturated organic compound) will
take place at a temperature of at least 630.degree. F. and a
pressure of 2,000 psi. In short, any form of chemical reaction in
an oxygen deficient material can be promoted and it is contemplated
that general water treatment, extractions of oil from sands or
shales, reduction of metallic ores and general molecular
degeneration of any material can be performed and accelerated. As
previously described, however, not all of these processes would
necessarily utilize water as a conveying medium or steam as the
heat energy.
What has been described herein is a hydraulic activation device
including those features which render the device satisfactorily
operable. However, certain devices which would be known to those
skilled in the art, such as chamber overflows, cleaning sumps,
automatic level controls, process performance monitoring,
irregularity alarms, cooling towers, gas separations, safety
valves, corrosion protection and other engineering devices have not
been described.
It can thus be seen that the apparatus and method disclosed herein
carry out the aforementioned objectives and otherwise improve the
high pressure chemical reactor art.
* * * * *